Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
  • B01J23/44—Palladium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
  • B01J31/06—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing polymers
  • B01J31/08—Ion-exchange resins
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
  • B01J31/06—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing polymers
  • B01J31/08—Ion-exchange resins
  • B01J31/10—Ion-exchange resins sulfonated
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
  • B01J31/165—Polymer immobilised coordination complexes, e.g. organometallic complexes
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
  • C01B15/01—Hydrogen peroxide
  • C01B15/022—Preparation from organic compounds
  • C01B15/023—Preparation from organic compounds by the alkyl-anthraquinone process
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
  • B01J2231/60—Reduction reactions, e.g. hydrogenation
  • B01J2231/64—Reductions in general of organic substrates, e.g. hydride reductions or hydrogenations
  • B01J2231/641—Hydrogenation of organic substrates, i.e. H2 or H-transfer hydrogenations, e.g. Fischer-Tropsch processes
  • B01J2231/643—Hydrogenation of organic substrates, i.e. H2 or H-transfer hydrogenations, e.g. Fischer-Tropsch processes of R2C=O or R2C=NR (R= C, H)
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/821—Ruthenium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/822—Rhodium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/824—Palladium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/825—Osmium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/827—Iridium
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
  • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
  • B01J2531/82—Metals of the platinum group
  • B01J2531/828—Platinum
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
  • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y10S502/00—Catalyst, solid sorbent, or support therefor: product or process of making
  • Y10S502/50—Stabilized
  • Y10S502/504—Abrasion resistance

Definitions

• the invention also includes the use of this hydrogenation catalyst in the production of hydrogen peroxide by a process of alternate hydrogenation and oxidation of a reducible quinone which is later oxidized to form the peroxide.
• the preferred range of surface area of the ion exchange resin is from 20 to 80 mF/g.
• This invention relates to the production of hydrogen peroxide, more especially to the production of hydrogen peroxide by a cyclic process involving alternate hydrogenation and oxidation of a reducible/oxidisable organic compound, and further relates to novel catalysts suitable for use as hydrogenation catalysts in such a cyclic process.
• platinum group metals have previously been proposed as hydrogenation catalysts for example for use in the hydrogenation step of a cyclic process for the producction of hydrogen peroxide involving alternate hydrogenation and oxidation of reducible/oxidisable organic compounds.
• the majority of such catalysts are of the metal deposit on carrier type, and in the great majority of cases palladium is the metal chosen and the variation has been in the carrier employed.
• materials proposed hitherto as carriers are activated alumina, activated magnesia, artificial aluminosilicates, titanium dioxide and cementitious materials.
• platinum group is meant ruthenium, rhodium, palladium, osmium, iridium and platinum.
• the present invention provides a catalyst material suitable for use in hydrogenation reactions, which catalyst essentially comprises a macroreticular ion exchange resin having a surface area of at least 5 m. g. carrying a deposit of one or more metals of the platinum group. Platinum, rhodium and palladium are the preferred metals for catalysts in accordance with the invention.
• the surface area of the ion-exchange resin is at least 20 m. /g., advantageously from 20 to 80 m. /g.
• the ion-exchange resin is of particle size not larger than 40 mesh B.S.S., suitably from 40- to 350' mesh B.S.S. desirably 50 to 200 mesh and advantageously from 100 to 150 mesh.
• Resin supports having such surface areas and particle sizes are especially preferred for hydrogenation catalysts which are to be employed in a cyclic process for the production of hydrogen peroxide.
• the method of preparing the catalyst material depends upon which of the metals of the platinum group is re- Patented Feb. 3, 1970 quired and further depends upon whether the macroreticular ion-exchange resin is in the cation or the anion form.
• cation and anion exchange resins each take either a strong form or a weak form according to the functional group of the resin. The description herein relates to both strong and weak form unless one or the other is specially mentioned.
• the form of an ion exchange resin is identified by reference to a functional group it is not intended to imply that all of the exchange sites on the resin are occupied by the group but only that the functional group named is the predominant one present.
• the present invention also provides process for the production of the novel catalysts comprising contacting the ion exchange resin with a solution containing ions of the metal or metals to be deposited thereon, removing the ion exchange resin containing absorbed metal ions from the bulk of the solution and reducing the absorbed ions to be corresponding metal.
• a solution containing ions of the metal or metals to be deposited thereon removing the ion exchange resin containing absorbed metal ions from the bulk of the solution and reducing the absorbed ions to be corresponding metal.
• a palladium nitrate/nitric acid solution is contacted with, for example, a palladium nitrate/nitric acid solution.
• the quantity of nitric acid is preferably no greater than the quantity required to prevent hydrolysis during the preparation. In this way competition by H ions for ion exchange sites is kept to a minimum.
• any other suitable composition may be employed, for example the sulphate/ sulphuric acid counterpart.
• a palladium chloride/hydrochloric acid solution giving rise to (PdCLQ- ions) or a hexachloropalladate solution, suitably of the potassium salt.
• reduction to palladium metal is necessary and can be effected with, for example, hydrogen (if suitable, in situ in the actual hydrogenation process for which it is to act as catalyst).
• a separate reducing agent can be employed, such as an aqueous solution of formic acid or sodium formate or formaldehyde, at a suitable temperature, from e.g. C. to boiling point, can be employed. It is possible to use an aqueous hydrazine solution for the reduction but it is found that it has a somewhat deleterious effect on the activity of the final catalyst.
• deposition of a cation exchange resin can be effected through the intermediary of cationic amine complexes, e.g. tetramine platinum (II) chloride and chloropentamine rhodium (III) dichloride.
• Reduction to the metal is suitably effected by thermal decomposition, e.g. at about 300 C., preferably in a nitrogen atmosphere.
• thermal decomposition e.g. at about 300 C., preferably in a nitrogen atmosphere.
• a convenient method is by way of hexachloroplatinic acid or sodium hexachlororhodate respectively each in aqueous solution.
• Reduction to the metal is suitably effected by the use of aqueous solutions of, for example, formic acid or sodium formate or formaldehyde or in the case of rhodium, in situ in a hydrogenation reaction as described above for palladium.
• aqueous hydrazine solution may be employed but with some loss of catalyst activity.
• the cation exchange resins should be in the alkali metal form, the strongly anionic exchange resins should be in the Cl form, and the weakly anionic ex change resins should be in either the free-base form or the Cl" form.
• the catalyst should contain at least 0.0025 g. atoms of metal per 100 g. of catalyst for instance from 0.0048 to 0.096 preferably 0.048 to 0.058 gram atoms of metal per 100 grams of catalyst Where rhodium, ruthenium or palladium are used and about 0.0026 to 0.052 preferably 0.026 to 0.031 gram atoms of metal per 100 grams of catalyst where osmium, iridium or platinum are used.
• Suitable macroreticular ion-exchange resins for use in preparing hydrogenation catalysts in accordance with the invention are styrenedivinyl benzene copolymer types such as those sold under the trade names (1) Amberlyst XN-1005- a strong cation exchange resin in the H+ form having a surface area of 122 m. /g.; (2) Amberlyst A-27, and A29 which are strong anion exchange resins in the C form, and A-Zl a weak anion resin in the free base form. These three materials have surface areas of 50 to 70 m. /g., 40 to 50 m. g. and 20 to 30 m. g. respectively.
• Suitable particle sizes are 40 to 350 (preferably 50 to 200) B.S.S. mesh and may, if necessary, be produced by grinding, or by otherwise reducing, particles of larger sizes.
• the exchange resin can be in the form of a process organic resinous material (having the required surface area of at least m. g.) which has been treated to absorb, for example, a compound having an -SO "I-l group, or a quaternary ammonium compound.
• Suitable cationic resins may advantageously be in the H+ form or particularly, in the Na+ or K+ forms.
• Suitable anionic resins may be in the Cl or OH" form or, particularly, in the S0 or C0 forms.
• the particular functional grouping desired may be achieved by treating ion exchange resins which are initially in a different from by known means so as substantially to replace the existing grouping by the desired grouping. Such replacement may be carried out either before, or after, deposition of the catalyst metal on the resin.
• properties possessed by a useful catalyst material are (a) good activity with respect to the desired reaction (b) good selectivity toward the desired reaction, and (c) good resistance to attrition and poisoning during use.
• the hydrogenation step involves suspending the catalyst in a solution of the compound (commonly an alkyl-substituted anthraquinone) to be hydrogenated and filtering the catalyst from the solution after hydrogenation.
• the compound commonly an alkyl-substituted anthraquinone
• catalysts in accordance with this invention have in comparison with the more important known catalysts comprising a platinum group metal on a support, a good combination of activity and selectivity. Certain of the catalysts also show a surprising resistance to attrition. Moreover, in the case of rhodium and, more especially platinum, a high and unexpectedly superior selectivity is observed toward the desired hydrogenation reaction.
• the Pt/anion-exchange resin catalyst particularly when employing the strongly anionic form, is an especially advantageous form in this respect. It has been observed that over a period of weeks the retention of activity of a Pt/anion exchange resin catalyst in accordance with the invention is appreciably superior to known Pd/alumina and Pd/ synthetic aluminosilicate catalyst. It does appear that the advantageous properties of the preferred catalysts in accordance with the invention do not stem solely from the use of an ion exchange resin or of a particular metal but from the combination of both these factors.
• Example 1 hereafter.
• This invention also provides processes for hydrogenation employing the novel catalysts and particularly such processes when part of a cyclic process for producing hydrogen peroxide.
• the solvent or solvent mixture used in the process may influence the selection of the ion-exchange resin employed for preparing the catalyst.
• the solvent is, or contains, an ester, such as a cyclohexanol ester
• a cation exchange resin in the form which may bring about some hydrolysis of the ester.
• an anion resin in the OH form there may be a liberation of Clions if any ion exchange takes place during use of the catalyst. This may be disadvantageous if apparatus which is prone to attack by Clions is used. Where such apparatus is used it may be desired, when using exchange resins originally in the Cl form to subject such resins, before use, to an ion-exchange reaction to replace Clions by other suitable ions.
• EXAMPLE 1 This example compares the selectivity of catalysts having supports according to the invention and catalysts using previously used supports for example alumina and artificial aluminosilicate with respect to the hydrogenation of 2-ethylanthraquinone (EAQ) or, where indicated, tetrahydro-2-ethylanthraquinone (H EAQ).
• EAQ 2-ethylanthraquinone
• H EAQ tetrahydro-2-ethylanthraquinone
• the corresponding hydroquinone is formed when 22.4 litres of hydrogen (at N.T.P.) have been taken up per mole of quinone.
• the hydrogenation was pursued substantially beyond the time taken for uptake of 22.4 litres. Further uptake beyond this volume corresponds to formation of nuclearly hydrogenated products and, eventually degradation products. Consequently the smaller this further uptake the beter, i.e. more selective, is the catalyst toward the desired reaction vis: the formation of hydroquinone only.
• the degree of hydrogenation is expressed as a hydrogenation factor a factor of 1.0 being equivalent to uptake of 22.4 litres of H at N.T.P. Therefore the nearer 1.0 the hydrogenation factor is the more selective the catalyst. In cases where the hydrogenation factor is quoted as 0 no hydrogen uptake at all was observed.
• EXAMPLE 2 This example compares the activity of various catalysts using supports according to the invention with those using supports previously known, such as alumina and a synthetic aluminosilicate. The tests involve reducing 8 g. of 2-EAQ in 100 ml. of 50/50 v./v. Aromasol/Sextate at room temperature using 0.15 g. of catalyst.
• EXAMPLE 3 This example compares the resistance to attrition shown by catalysts or supports according to our invention in comparison with a synthetic alumino-silicate catalyst.
• resins were in the form of spheroidal beads while the alumino silicate had a granular form.
• a quantity of the catalyst or catalyst support was suspended in a 50/50 v./v. mixture of aromasol and sextate in a glass cylinder having a bore of 3.8 cms. and a ground 30 inner surface.
• a stainless steel rotor having a diameter of vessel and made up to a fixed volume with further solvent.
• EXAMPLE 4 For the preparation of a palladium-anion resin catalyst an aqueous slurry was made of Amberlyst A-27 resin in the chloride form and of size range -l +150 mesh B.S.S. and sufficient palladium chloride to give 5% metal in the final product. The slurry was slightly acidified with hydrochloric acid to prevent hydrolysis.
• the slurry was stirred for 20 minutes and the resin was then filtered free from supernatant liquor and washed with demineralised water.
• the resin was then treated to reduce the palladium to the metallic state.
• the water-wet resin was added to a boiling solution of sodium formate (2O g./l.) in demineralised water. Boiling was continued for 30 minutes during which time further additions of solid sodium formate were made until vigorous effervescence on addition of sodium formate ceased.
• the mixture was cooled, filtered and the palladised resin washed with demineralised water and dried.
• EXAMPLE 5 The preparation described in Example 4 was repeated up to the palladium reduction step. In the present example that step was conducted by drying the moist resin by displacing imbibed water with acetone and then removing the acetone in the oven at 70 C. The dry resin was then placed under benzene (or other inert solvent) and shaken with hydrogen in the usual way. When hydrogen uptake ceased the reduction was complete and the catalyst was dried.
• EXAMPLE 6 The preparation described in Example 4 was repeated up to the palladium reduction step.
• the reduction step was conducted by adding the watermoist resin to a solution of excess formaldehyde in demineralised water at 70 C. When reaction was complete the solution was cooled, filtered and the palladised resin dried.
• EXAMPLE 7 For the preparation of a rhodium-anion resin catalyst, the procedure of Example 4 was adopted, employing an aqueous solution of sodium hexachlororhodate.
• EXAMPLE 8 For the preparation of a platinum-anion resin catalyst the procedure of Example 4 was adopted, employing an aqueous solution of hexachlorplatinic acid.
• EXAMPLE 9 In the case of a platinum-cation resin catalyst use was made of Amberlyst XN-1005 in the Na+ form and of size range -60 +85 mesh B.S.S. The procedure was as in Example 4 as far as the reduction step, except that an aqueous solution of tetramine platinum (II) chloride was employed. In this case reduction was effected by heating the product to 300-310 C. in an atmosphere of nitrogen.
• a catalyst material suitable for use in hydrogenation reactions, essentially comprising a macroreticular ion exchange resin having a surface area of at least 5 m.'-/g. carrying a deposit of a metal selected from the group consisting of ruthenium, rhodium, palladium, osmium, iridium and platinum or a combination of any of these metals.
• a catalyst material as claimed in claim 1 wherein the ion exchange resin has a surface area of from 20 m. /g. to n1. /g.
• a catalyst material as claimed in claim 1 wherein the ion exchange resin has no particles smaller than 350 mesh B.S.S.
• a catalyst material as claimed in claim 1 wherein the ion exchange resin comprises particles of from 200* mesh 8.3.3. to 50 mesh B.S.S.
• a catalyst material suitable for use in hydrogenation reactions, essentially comprising a macroreticular anionic or cationic exchange resin having a surface area of at least 5 m./ g. carrying a deposit of ruthenium, rhodium, palladium, osmium, iridium or platinum or any combination thereof.
• a catalyst material as claimed in claim 6 wherein the resin is the Cl, OH: SO or C0 form.
• a catalyst material as claimed in claim 6 wherein the ion-exchange resin carries a total deposit of from 0.0048 to 0.096 gram atom of one or more of rhodium, ruthenium or palladium per 100 grams of catalyst.
• a catalyst material suitable for use in hydrogenation reactions, essentially comprising a macroreticular anionic exchange resin in the C1, OH", 80 or CO form, having a surface area of from 20 mF/g. to 80 m. g. and consisting of particles of from 200 mesh B.S.S. to 50 mesh B.S.S. carrying a deposit of from 0.0026 to 0.052 gram/atom of platinum per 100 g. catalyst material.
• a process for the production of a catalyst essentially comprising a macroreticular ion-exchange resin having a surface area of at least 5 mfi/g. carrying a deposit of one or more of the metals ruthenium, rhodium, palladium, osmium, iridium and platinum comprising contacting the ion exchange resin with a solution containing ions of the metal or metals to be deposited thereon removing the ion exchange resin containing absorbed metal ions from the bulk of the solution and reducing the absorbed ions to the corresponding metal.
• a process for the production of a catalyst essentially comprising a macroreticular ion-exchange resin having a surface area of at least 5 m. g. carrying a deposit of one or more of the metals ruthenium, rhodium, palladium, osmium, iridium and platinum which comprises contacting the ion-exchange resin with a solution containing ions of the metal or metals to be deposited thereon, removing the ion-exchange resin containing absorbed metal ions from the bulk of the solution and reducing the absorbed ions to the metal by means of an aqueous solution of formaldehyde, formic acid or sodium formate.
• a process for the production of a catalyst essentially comprising a macroreticular ion-exchange resin having a surface area of at least m. g. carrying a deposit of one or more of the metals ruthenium, rhodium, palladium, osmium, iridium and platinum which comprises contacting the ion-exchange resin with a solution containing ions of the metal or metals to be deposited thereon, removing the ion-exchange resin containing absorbed metal ions from the bulk of the solution and the absorbed ions are reduced to the metal in the hydrogenation reaction to be catalysed.
• a process for the production of a catalyst essentially comprising a macroreticular cation exchange resin having a surface area of at least 5 m. /g carrying a deposit of rhodium or platinum which comprises contacting the resin with an aqueous solution of chloropentamine rhodium dichloride or tetra-amine platinum chloride respectively, removing the resin from the bulk of the solution and reducing the absorbed complex to metal.
• a process for the production of a catalyst essentially comprising a macroreticular ion-exchange resin having a surface area of at least 5 m. g. carrying a deposit of one or more of the metals ruthenium, rhodium, palladium, osmium, iridium and platinum comprising contacting the ion exchange resin with a solution containing ions of the metal or metals to be deposited thereon, removing the ion exchange resin containing absorbed metal ions from the bulk of the solution and reducing the absorbed ions to the corresponding metal whereafter the catalyst is treated with an alkali.
• a process for the production of hydrogen peroxide which comprises hydrogenation of a quinone in the presence of a catalyst as claimed in claim 1 wherein the hydrogenation is a part of a cyclic process for the production of hydrogen peroxide involving alternate hydrogenation and oxidation of the quinone.
• reaction solvent contains a cyclohexanol ester.

Landscapes

• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Materials Engineering (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Inorganic Chemistry (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Catalysts (AREA)

Applications Claiming Priority (1)

Publications (1)

Family

ID=10454986

Family Applications (1)

Country Status (8)

Cited By (10)

Citations (6)

• 1965
  • 1965-11-25 GB GB50184/65A patent/GB1146437A/en not_active Expired
• 1966
  • 1966-11-18 NL NL6616305A patent/NL6616305A/xx unknown
  • 1966-11-21 SE SE15920/66A patent/SE330002B/xx unknown
  • 1966-11-22 FI FI663077A patent/FI46327C/fi active
  • 1966-11-22 US US596094A patent/US3493343A/en not_active Expired - Lifetime
  • 1966-11-24 BE BE690125D patent/BE690125A/xx unknown
  • 1966-11-24 FR FR84820A patent/FR1502268A/fr not_active Expired
  • 1966-11-25 DE DE19661567650 patent/DE1567650A1/de active Pending

Patent Citations (6)

Also Published As

Similar Documents